Conversion of hydrocarbon oils



March 6, 1934. G, EGLOFF 1,949,460

CONVERSION OF HYDRCCARBON OILS Filed March 5, 1931 FRACTIONATOR FURNACE 26 INVENTOR GUSTAV EGLOFF Patented Mar. 6, v t

1,949,4t'c convcasron or HYDROCARBON OILS Gustav Egloff, Chicago, Ill., assignor to Universal Oil Products Company, Chicago, 111.,- a corporation of South Dakota Application March 3, 1931, Serial No. 519,872 1 Claim. (01. lee-5t) This invention relates to the treatment of in part )through valve 5. in line 4, and through hydrocarbon oils and particularly refers to the line 6 and valve 7 into fractionator 8. Preferably conversion of hydrocarbon oils into lighter and all or a portion of the raw oil charging stock more valuableiproducts. passes either through line 9 and valve 10 into 5 Primarily the invention comprises preheating preheating coil 11 or through valves 5 and 12, in 609 raw oil charging stock for cracking by indirect line 4, through preheating coil 13, line 14, valve contact with relatively hot residual oil within a 15 and line 9 into preheating coil 11. The raw reaction chamber of a cracking system and thence oil, if any, supplied through line 6 and valve '7 supplying the preheated raw oil to the same to line 8 may be preheated by direct contact with 10 cracking system for conversion. the relatively hot vapors undergoing fractiona- 85 As a feature of the invention the preheated tion in this zone. Preheating coil 13, as here raw oil may be supplied to the heating element illustrated, may be located in fractionator 8 and of the cracking system at any one or a plurality the raw oil, if any, fed therethrough may be pre-- of points including the inlet to the heating eleheated by indirect contact with the vapors in it ment, the discharge from the heating element as this zone. It will be understood that preheating to well as intermediate points within the heating coil 13 may or may not be used, as desired, and element. that other well known means of preheating the Among the benefits which may be derived by raw oil charging stock may be employed instead preheating the raw oil in the manner provided of or in conjunction with the method illustrated.

so by the present invention the residual liquid prod- Preheating coil 11 may be located within the" as nets of conversion are preferably cooled sumlower portion of reaction chamber 16 and preferciently to prevent deleterious secondary reacably a portion or all of theraw oil charging stock tions within the body of-residual liquid in the is supplied thereto. as previously indicated. The reaction chamber d m thus obviate the exraw oil is indirectly contacted in preheating coil as .cessive formation of coke or carbonaceous ma- 11 with the relatively hot residual liquid within as terial and generally imp v the q li y of the chamber 16 serving to cool the residual oil and residual Product r d y he y m being thereby preheated. The preheated raw In its more specific e bodi e the inve tion oil from preheating coil 11 may pass through line m y p i subjecting y r r n 11 to 17 and may be subjected to conversion conditions at v r i i n in a heating nt. in roby being fed into the cracking system in one or 5 duoi s the hea d p s nto an enlar ed rein any combination of several manners. Preaotion zone where vapors may be separated from heated raw oil may, for example. pass from line d l 11. subie'ctingthe V p t0 fractionfl- 17 through line 18 and valve 19 into line 20 and tion. r urnin th r l iv l heavy insuflioien ly thence to heating element 21 or it may pass converted components of the vbpols'to the a through line 22 and valve 23 into line 52 which ins ele nt for Ver$ion.-subiecti 8 t e eis the discharge line from heating element 21 tlvelr li fractionated Vapors, t0 condensation or preheated raw oil may pass through one or a and coo a d col ecting the resulting products. plurality of lines 24- controlled by valves 25 into subjecting w 011 charging Stock for thesystem "any desired intermediate point or points in heatgp to indirect contact with the relatively hot residm element 21,

I151 011 Within the reaction chamber and p y- Heating element 21 may be located within any ins the pr h w n ei r int the inlet suitable form of furnace 26 and the oil supplied 7 to the heating element or into the discharge from thereto may beheated to any desired conversion the heating element or into one or a plurality of temperature preferably under a substantial su- 45 intermediate points in the heating'element or in peratmospheric pressure. The heated oil may any. combination of these mariners as desired. be discharged through line 52, valve 2'7 and valve The tt h d i r u drawing m t t 28 into reaction chamber 16.- Separation of one form of apparatus incorporating the prinvapors andresidual oil maybe effected in chambiples of the present invention. The following her '16. The residu l l m y be Withdrawn to 60 description of the drawing embraces also a destorage or to further treatment, as desired,

scription of the process of the invention as it through line 29 and valve 30. Vapors from chammay be. practiced in the apparatus illustrated. ber 16 may'pass through line 31 and valve 32 Raw oil charging stock may be supplied through to be subjected to fractionation in fractionator 8. line 1 and valve 2 to pump 8 from which it may Insufllciently converted components of the vapors 66 be fed through line 4 and may, if desired, pass subjected to fractionation may be condensed in the fractionating zone and supplied through line 33 and valve 34 to pump 35 which preferably returns this product together with any desired portion of the raw oil charging stock which may have been fed directly into th fractionator, as previously described, through line 20 and valve 36 to heating element 21 for reconversion. Relatively light fractionated vapors of the desired composition may pass from fractionator 8 through line 37 and valve 38 to be subjected to condensation and cooling in condenser 39, products from which may pass through line 40 and valve 41 to be collected in receiver 42. Uncondensable gas may be released from receiver 42 through line 43 and valve 44. Distillate may be withdrawn through line 45 and valve 46. A portion of the distillate may, if desired, be withdrawn from receiver 42 through line 47 and valve 48 to pump 49 to be recirculated through line 50 and valve 51 to fractionator 8 to assist fractionation of the vapors in this zone.

Pressures employed within the system may range fromsubatmospheric to superatmospheric residual oil in the lower portion of the reaction chamber, is introduced in part into the upper portion of the heating element and in part into the discharge from the heating element. The refluxcondensate from the fractionator of the system is subjected in the heating element to a maximum temperature of about 975 F. but this temperature is decreased by the introduction of raw oil and the stream of heated products entering the reaction chamber is at a temperature of about. 900 F. The heating element is maintained under a superatmospheric pressure of approximately 250 pounds per square inch and this pressure is substantially equalized throughout the succeeding portions of the system.

This operation may yield approximately 55 percent of motor fuel having an anti-knock value approximately equivalent to a blend of 50 percent benzol and 50 percent Pennsylvania straightrun gasoline. About 10 percent of pressure distillate bottoms and some 28 to 30 percent of marketable fuel oil may also be produced. The remaining 5 to 7 percent is chargeable to gas and a negligible percentage of carbon.

I claim as my invention:

In a cracking process of the character wherein hydrocarbon oil is maintained under cracking conditions of temperature and pressure in an enlarged reaction zone and vapors removed from the reaction zone and subjected to fractionation, the method which comprises preheating a portion of the charging oil for the process by heat exchange with the vapors undergoing fractionation, passing the thus preheated charging oil, in admixture with reflux condensate formed by the fractionation, to a'heating zone and heating the same to cracking temperature under pressure while flowing in a restricted stream through the heating zone, discharging the hot oil stream into said reaction zone, passing another portion of the charging oil for the process in indirect heat exchange relation with hot liquid oil con stituents in the reaction zone whereby it is preheated to higher temperature than the firstmentioned portion of the charging oil, and then 'combiningsaid other portion of the charging oil with said hot oil stream discharging into the reaction zone.

GUSTAV EGLOFF. 

